Process and apparatus for refining petroleum oil



Feb. 27, 1923.

` J. C. BLACK PROCESS AND APPARATUS FOR REFININC- PETROLEUM OIL if ...oEw:

Filed June 20,

Feb. 27, 1923.

J. C. BLACK PROCESS AND APPARATUS FOR REFINING PETROLEUM OIL Filed June20, 1922 2 sheets-sheet ..50 m. .QZ

@noe/Mofa Jaim lac/f,

Patented Feb. 27, 1923.

UNITED STATES JOHN C. BLACK, OF, DESTREHAN, LOUISIANA, AASSIGNOR FONE-.HALF WEIR, OF'FILLMORE, CALIFORNIA. i

`:PROCESS AND APPARATUS FOR REFINING PETRLEUH OIL.

l 1,447,118 PATE-Nr or-r-lci-z. l

.Application led June 20, l1922. Serial'No. 569,751@

To all 'whom 'it may concern.'

Be it known that I, J oHN C. BLACK, a citizen of the United States,residing at Destrehan, St. Charles Parish, Louisiana, have inventedcertain new and useful Improvements in Processes and Apparatus forRcfining Petroleum Oil, of which the follow- 'ingis a specification.

-This invention relates to the art of refining petroleum oil and to anapparatus for practicing the same, more particularly to the separationor fractionation of the distillates therefrom. v

To illustrate the novel features of my invention, I show in Figure l ofmy drawing a part elevation part section ofmy fractionating apparatusand in Fig. 2 a modiication thereof, which together with myspecification will disclose the principle of operation and the method ofapplication to a particular case but which fairly represents thevprocess. It is to ,be understood, however, that my invention is of muchwider scope than the single application shown, as I have employed it forthe fractionation of all grades of distillates from the lightestgasolines to the heaviest grades of so-called paraiine distillate havinga range of boiling points under 100 F. tol

over 600 F.

The disclosure is susceptible of considerable modification to suitparticular requirements, but the underlying principle of operation isthe same.

It has sometimes been customary heretofore in fractionating oils todistil the crude oil and pass the vaporsthrougha tower or tank havingcooling tubes extended therethrough. These tubes were usually kept coolby passing air through them. The cooling tubes would cool down thedistilled vapors in the tower or tank and liquefy those having thehighest boiling points. leaving the vapors of the low boiling point oilsto pass out the. upper part of the tower -In this previous process itwas. diiiicult to regulate the temperature ofthe cooling tubes and hencethe amount of vaporized oil fractions that leave-'the tower. Moreoverthis fraction took over with it various impurities which ohjectionalblydiscolored the oil fraction when finally condensed. I have discoveredthat a much more efficient control and a distillate of better qualitycan be secured by what I conveniently denominate my'wash method. if

I prefer to use as a wash oil in this process hydrocarbons of similarphysical properties to those I wish to separate from the vapors to betreated, fortwo reasons, rst

by so doing the effluent from the washing section of the tower willje ofsubstantially constant quality and can be used in a cycle of washoperations without material change 1n the properties of the wash oil,and second, oils of similar properties act in a. more eiicient manner assolvents for each other, and their mixtures. or. solutions .are morestable than oils of dissimilar properties.`

' Furthermore by washing and condensing out the heavier or higherboiling point fractions, particularly the heavy paraffine distillates,at the high temperature prevailing in `the washV chamber, the steam orwater "apor will remain in the vapor form and condense with the light orlow 4boiling fraction from which it will readily separate, therebyobviating the troublesome emulsions when the heavy distillatesarecondensed with the water in them. if there are no light distillatesthen the water will condense out as a separate condensate. i

To more particularly describe my process and show itsv application in asimple form, reference is made to the drawing in ,which it will be seen1 represents an evaporatoror vaporizing chamber but which is not es'sentlal to the lnvention as any source of vapor such asa still. would beequally suitable.. but is merely shown for illustratlve purposes, 2 is avapor line. connecting the evaporator to thel fractionating tower 3; 4

is a vaporline connecting the upper part of the tower wth the washingsection of the tower 5; 6 is a vapor line connecting the aipperportionof the washing section of the tower with the vaporV condenser 7,-and Ythrough proper piping to the light oil tank 37 8 and 8 are draw-offlines connected -with the bottom of the wash section 5 and" the uppersection 10,'the wash section 5 and the upper section 10 are separated bya diasyphon breaker in the riser-15; 16 is a line leading to theobservation or look box 1 7 and 18" is a connection to the tank 19; 201s a connection from the tank'19 to the pump 21; 22 is a dischargeline/from the pump to the sprinkler head- 23 and is fitted with acontrol valveA 24; 25 is a suction line from tank 19 to the pump 26which in turn is connected to the discharge line 27 and to the storagetank 28; 29 are wash plates or preferably spiral tiles; 30 are bafileplates 1n the upper section of the tower; 31 are perforated trays in theevaporator. and 32 is a steam spray line. 34 is a gas vent in line 33connecting the condensing coil 7 through pipe 36 to the Light Oil Tank37. 38 is a water separatingtrap vin the pipe 33 d1scharging into sewer39.

I will now describe the operation of the apparatus in carrying out myprocess of fractionation, it being assumed that the tower is operatingon vapors from a continuous source of supply and are of substantiallyuniform constitution and also that tank 19 is supplied with sufficientwash oil to start the operation.

The hydrocarbon vapors mixed more or less with water vapor or steam passout of the still or evaporator 1 through the vapor line 2 into the lowerportion of the separator 10, which is fitted with baffle plates 30 tocatch any entrained heavy oil that might be in the vapor stream, thisseparated oil is drained away through the drain line 8 and is either runinto line`8 and to the cooler coil 12 or back to the source of vaporsupply through the line 9 by the proper manipulation of the valves 8"and 9. From the separating chamber 10 the vapors now pass through pipe 4to the lower portion of the washing chamber 5. Here the vapors inascending to the outlet pipe 6 meet with a washing operation in whichthe higher boiling point hydrocarbons are separated from the lowerboiling constituents of the vapor by condensation and absorption broughtabout by the cooling and absorption effect of the same or similar oilinjected or sprayed into the washing chamber through the spray pipe 23supplied from the pump 21 through line 22 and control valve 24, the pumpin turn taking suction through line 20 to tank 19 which in turn takesits supply from the oil drained away from the tower through line 8 andcooler 12. The spray oil or wash oil is sprayed over the wash tileswetting their surface with a cooling medium and offering a large wettedsurface for the condensation and absorption of the high boilinghydrocarbons similar in physical properties to the wash oil which afterdraining away through line 8 and cooler 12 and tank 19 may be returnedto the tower as the washing oil, this operation being a continuous one,the excess accumulation of oil in tank mamie to the tower is undercomplete control of the operator by regulation of the control valve 24and by such contrcl he can regulate the cooling, condensing andabsorption etfec-t of the tower and by so doing he can obtain anydesired vaporization product through line 6 and condenser 7 that hedesires within the limits of the apparatus, or it may be advanta eous toso regulate the wash oil as to con ense or absorb the "fractions desiredirrespective of the vapor passing out of the tower or to another washcompartment.

It is not essential to the successful operationfof the apparatus to havethe separator chamber on top of the wash chamber but .may be reversedand be underneath as shown in Fig. 2, and in some respects it will sim-`plify the construction to be so assembled, or the separator may be aseparate chamber altogether and may be connected to the wash chamber bypipe connections only. Furthermore, the washing chamber may bemultiplied to any number desired, as shown diagrammatically in Fig. 2,each chamber yielding a different fraction, each'chamber being sprayedlwith wash oil previously 0btained from the same chamber, cooled andreturned thereto. In this way the various fractions do not becomecontaminated with other fractions having diierent physicalcharacteristics.

It is to be understood that each washing chamber will have itsindependent draw-olf and independent cooler, look box, tank, pump andlines to accomplish the result above stated, the corresponding numbersin Fig. 1 and Fig. 2 show similar' elements of the apparatus.

In my application 569757 for the fractionation of crackedhydrocarbons, Ishow a fractionating tower embodying the above described principle ofoperation in which form separate fractions are produced, each havingdifferentv boiling points, gravity, volatility and other physicalproperties.

From the storage tank 28 which is the storage for the excessaccumulation from tank 19 is a connection 44 and valve 43 leading t'othe pump 45 which in turn discharges into the still 46; connected to thestill is the vapor line 47 running through the cooler 48 to the look box49, and pipe 50 to the tank marked Heavy lNaphtha. Connected to theHeavy Naphtha tank and the Light Oil Tank 37 is a pump 52 which drawsthe collected hydrocarbons through pipes 51 and valve 51 and pipe 53 andvalve 53 respectively. Pump 52 dis- Residue connected tothe evaporator 1by the pipe 41, valve 41 and valve 40.

The operation that takes place in the above apparatus is as follows: Theexcess .wash oil and condensate from the tower and accumulated' in tank19 is pumped to tank 28 by the pump 26. The oil in tank 28 containscertail of the heavy fractions from the vapors passing throughl the washtower and also some of the lighter intermediate fractions. To separa-tethese fractions and rccover the more valuable light fractions they arepumped Vinto the still 46 wherein the light fractions are distilled offand condensed and run to the Heavy Naphthaf tank and the residue .in thestill is run to the Gas Oil Tank through the lines 60 and 62 and pump 61to be disposed of as a separate commodity. The heavy naphtha collectedin the Heavy Naphtha tank is now blendedwith the lighter naphtha in tank3:? by the operationof the pump 52 taking from each tank the properpercentage of each in the proportion in which they are produced to makethe blend or mixture in tank 56. The oil in tank 56 is the finishedproduct of this particular process.

The residue .in the still or evaporator 1 is stored in tank 42 and isusually disposed of as fuel oil. One of the objects of this invention isto extract a larger amount of the light or more volatile fractions ofthe oil under treatment thereby giving the residue a higher flash pointthan heretofore and also to increase the yield of the lighter fractionsby more thorough fractionation and separation of the vaporizedhydrocarbons. Y

Another object of this invention is to make an improved finishednaphtha, that is to say, I am enabledto obtain a cleaner, water-free andbetter colored naphtha than Iheretofore and also to greatly improve theboiling points of the naphtha to the end that it makes a more valuableproduct for the production of gasoline.

Having now described my'process of fractionation and apparatus forcarrying itinto effect, what I claim as new and desired'to securebylLetters Patent is the following:

1. The process of fractionally separating mixed-oil vapo'rs obtained bydistillation of oil comprising continuously circulating from a-'sourceof supply to a mixing compartnent a liquid hydrocarbon of approximatelythe same composition as the oil fraction which it is desired to separateout and bringing it into intimate contactwith the mixed oil vapors toliquefy and separate from vthe residual vapors the fraction havingsubstantially the same composition as the circulated hydrocarbon.

2. The process of fractionally se arating mixed oil vapors comprisingycontinuously circulating,T a liquid hydrocarbon of a proximately the-same composition as t e oil fraction which it is desired to separateout and bringing it into intimate contact with the mixed oil vapors toliquefy and separate from the residual vapors, the fraction havingsubstantially the same composition as the circulated hydrocarbon andcondensing the residual vapors.

3. A process of fractionating mixed hydrocarbons of different physicalproperties consisting in washing, cooling, absorbing and separatingfractions from a vapor containing them with washing, cooling andabsorbing hydrocarbons of similar physical properties, conduct-ing awaythe solvent and its dissolved hydrocarbons, cooling them,`

and returning a portion of the cooled hydrocarbons to the chamber fromwhich they were withdrawn to be used again as a washing, cooling 'andabsorbing medium for the hydrocarbons of similar physical properties,and condensing the residual vapors. l

4. The process of, separating 4from a mixed vapor obtained bydistillation of oil, hydrocarbons of certain properties containedtherein, which consists in washing, cooling, condensing and absorbingthe fraction of the hydrocarbon vapor having Said properties by a cooledhydrocarbon having the same properties, conducting the condensate to astoragecompartment and drawing from the storage compartment thecondensate and again bringing it into contact with fresh supplies ofthemixed oil vapors to wash, cool, condense and absorb that fraction of themixed vapor having the ysame roperties as the condensate, conducting tiecondensate again to the same storagecompartment and repeating the cycleof operation as set forth. y

5. The process of separating mixed hydrocarbons having different boilingpoints comprising vaporizing the hydrocarbons and washing the vaporswith a hydrocarbon having substantially the same boiling point and otherphysical characteristics as the hydrocarbons desired to be separated outto thus liquefy the hydrocarbon and then liquefying other liquefiablevapors of the remaining mixed hydrocarbons.

6. The process of fractionating mixed hydrocarbons which are normallyliquefied at atmospheric temperatures, but which have different boilingpoints, comprising vaporizing the hydrocarbons, washing the vapors witha liquid hydrocarbon of substantially the same composition and boilingpoint as the fractions to be separated in order to liquefy and absorbthe same, conducting the condensate to a storage compartment, thenbringing the condensate from the storage compartment and passing it intolntlmate contact with fresh supplies of the mixed hydrocarbon vapors tocondense that fraction of the vapors having the same properties as thecondensa-te and in turn conducting the condensate to the storagecompartment and continuously repeating this cycle of operation asdescribed.

'i'. The process ofrfractionating mixed hydrocarbons normally liquefiedat atmospheric temperatures but having different boiling points,comprising vaporizing the hydrocarbons and washing the vapor with aspray of liquid hydrocarbons simllar in boiling point and other physicalcharacteristics of the fraction to be separated and separating theunliquefied vapors and the liquefied hydrocarbon fraction as described.

8. The process offractionating mixed hydrocarbons normally liquefied atatmospheric temperature, but having different boiling points comprisingVaporizing'the hydrocarbons, washing the vapors liquefying' andseparating therefrom a fraction With a lipuid hydrocarbon having similarboiling points and other physical characteristics as those of thefraction separated, separating the remaining vapors and liquefiedfractions by conducting the liquefied fractions to a storage compartmentand continuously drawing from the storage compartment fresh supplies ofthe liquefied fractions and using the liquefied fractions as a wash oilto liquefy other vapors being treated, as described.

9. |The process of fractionating mixed hydrocarbons of different boilingpoints coniprising vaporizing the hydrocarbons and spraying the vaporswith a liquid hydrocarbon having substantially the same boiling pointsand other physical characteristics as the fraction desired to beseparated, separating the residual vapors and the liquefied fractiontogether with the admixed wash oil,v conducting the liquefied fraction`together with the admixed wash oil to a storage compartment,continuously returning a portion of the liquefied fraction and wash oil,and using the admixed liquefied fraction and wash oil to liquefy andcondense other vapors containing fractions having substantially the Sameproperties.

l0. The process of ractionating hydrocarbons having different boilingpoints and other physical characteristics consisting in washing thehydrocarbons while in a vapor form with a liquid hydrocarbon havingsubdensing effect will be such Lacalle stantially the same boiling pointandother physlcal characteristics as the fraction to be separated,.regulating the supply of liquid hydrocarbon in the washing step wherebythe washin and liquefying effect Will be such as to hquefy and separatefrom the vaporfthe hydrocarbons having substantially the same boilingpoint and other similar physical characteristics to those'of the washhydrocarbon' so that the wash hydrocarbon together with the admixedcondensate will have a similar boiling point and other physicalcharacteristics to the original Wash hydrocarbon and afte cooling may beagain used as the wash hydrocarbon ina cycle of washing operationswithout material change 1n lts Washing and liquefying effect, and thencondensing the residual washed and liquefied vapors. I

11. A process of treating rhydrocarbons consisting in subjecting thehydrocarbons while in a vapor form yto a Washing2 coollng and condensingaction by a liquid hydrocarbon wash oil, regulating the supply of liquidhydrocarbon inthe Washing compartment whereby the washing, cooling andconand separate from the vapor the hydrocarbons having similar physicalproperties to those of the wash oil so that the wash oil together withthe admixed condensate will'v have similar physical properties to theoriginal wash oil and after cooling may be again used las the wash oilin a cycle of Washing operations Without material change in its Washing,cooling and condensing effect, then passingvthe uncondensed vapors to asimilar washing, cooling and condensing compartment wherein anotherfraction is condensed and separated, but having a lower specific gravitycorresponding to the lower specific gravit-y of the wash oil, andseparately condensing the residual vapor.v

12. An apparatus for treating hydrocarbons comprising a tower2 means.for supplying hydrocarbon va )ors to said tower, a source of supply ofliquid hydrocarbons, means to circulate the hydrocarbons from the.supply source through the tower back to the supply source, a cooler tocause the liquid and vapor forms of hydrocarbons to come into intimatecontact whereby some of the hydrocarbon vapors are liquefied andabsorbed by the liquid hydrocarbons, a condenser and an outlet. tubeextending from the tower t0 the condenser to condense the remainingunliquefied vapors.

In testimony whereof I hereunto afiix my signature.

- JOHN 'C. BLACK.

as to condense i

